CN102908877B - Gas-liquid membrane contactor and mixed gas separation method using same - Google Patents
Gas-liquid membrane contactor and mixed gas separation method using same Download PDFInfo
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Abstract
The invention relates to the technical field of membrane separation, in particular to a gas-liquid membrane contactor and a mixed gas separation method using the same and solves the problems of unstable mass-transfer efficiency, difficulty in assembling and high cost of existing gas-liquid membrane contactors. The gas-liquid membrane contactor is of a tube shell type rectangular structure consisting of a hollow fiber membrane and a frame. The hollow fiber membrane is a tube pass for delivering air, the rectangular frame is a shell pass for delivering liquid, fair current, countercurrent, cross current separation can be achieved selectively, and the shortages of uneven distribution density of hollow fibers and uneven shell pass liquid are effectively avoided. Therefore, the gas-liquid membrane contactor is better than existing hollow fiber membrane contactors, and the separation efficiency is improved by 20-38 percent.
Description
Technical field
The present invention relates to technical field of membrane separation, particularly a kind of gas-liquid membrane contactor and apply its mist separation method.
Background technology
Gaseous mixture comprises various process gas flow and flue gas etc. in industrial production, such as natural gas, synthesis gas, refinery gas, Claus tail gas, flue gas of power plants and flue gas, and containing various harmful foreign gas in these mists, modal foreign gas has H
2s, SO
2and CO
2deng sour gas and VOCs, before these air-flows are further processed or discharge, purified treatment must be carried out, the foreign gas (such as sour gas and VOCs etc.) that removing is wherein harmful, to meet requirement or the environmental emission standard of follow-up workshop section.The advantages such as membrane contactor is a kind of new gas separator, and it has stable mass transfer interface, high-specific surface area, high mass transfer efficiency, and energy consumption is low, and the little and operating flexibility of device volume is large.Its separator as a kind of advanced person is widely used in the fields such as Chemical Engineering, environmental project, food industry and medical industry.At current energy source growing tension, under the situation that environment is increasingly severe, the energy-efficient theme having become various countries' technical development.Therefore the exploitation of membrane contactor is subject to the great attention of various countries.
Membrane contactor is because it is in mass transfer area, mass-transfer efficiency, the aspects such as the size of operating flexibility, device have outstanding advantage, be subject to the great attention of countries in the world researcher, be considered to have one of very large application potential and the technology being expected to alternative traditional gas absorber (as tower etc.).The membrane contactor with practicality of current exploitation, comprises hollow fiber film assembly and plate film assembly, and the former structure has flat flow and cross-current type two kinds, and the latter has spiral etc.Flat flow feature is the flow direction of gas-liquid two-phase is parallel, and be divided into and flow and adverse current, this assembly is easily manufactured, and price is lower, and shortcoming is that the doughnut distribution density of filling is uneven, affects being uniformly distributed of shell-side fluid.Cross-current type feature is the flow direction of gas-liquid two-phase is intersect, the acquisition of cross-current can adopt direct cross-current configuration and deflection plate to force form, the advantage of cross-current type hollow fiber film assembly is doughnut distribution uniform, cross-flow makes fluid velocity flow direction vertical with fiber surface, thus strengthen mass-transfer efficiency, its shortcoming is assembling difficulty, and cost is higher.Spiral membrane module is by ready-made Flat Membrane sealing film forming bag, serves as a contrast with netted interval insulant and is closely wound on porous central tube and make between two film bags.The compact conformation of spiral membrane module, the effective film area of unit volume is comparatively large, and manufacture craft is relatively simple, installs and operates also more convenient.Be adapted at low flow velocity, operate under low-pressure.But it is due to not easy cleaning, higher to the pre-processing requirements of raw material.The advantages such as hollow fiber film assembly can provide high packed density, good pressure-resistant performance, large specific surface area, compact conformation, easy to make, therefore, application is higher than other assembly.The people such as Hoff develop cross-current type hollow fiber film assembly, have studied it and absorb CO
2process, determine mass transfer flux, two-dimensional diffusion-reaction model can prognostic experiment result; The people such as Dindore determine hollow fiber membrane contactors shell-side diffusion coefficient, for the design of membrane module provides foundation.UBE company of Japan, CHUB company and NIPPON company etc. all develop hollow fiber film assembly, and it is mainly used in CO in flue gas
2recovery.Kvamer company of Norway develops a kind of for separating of CO in natural gas
2membrane absorption method technique, this technique can apply flat and hollow fiber film assembly.United States Patent (USP) (USP7318854B2) proposes CO in a Selective Separation gaseous mixture
2membranous system, this system adopt hollow fiber membrane contactors.The colleges and universities such as domestic Zhejiang University, University Of Tianjin, Beijing University of Chemical Technology and Nanjing Information engineering Univ have carried out more research in membrane contactor application aspect.
Membrane contactor is a piece-rate system in essence, and its high efficiency relates to membrane material and membrane contactor structure, and wherein membrane contactor structure is energy-efficient key, is also the basis of improving the market competitiveness.Therefore the meaning that energy-efficient membrane contactor has particular importance is developed.At present, it is uneven to there is doughnut distribution density in the membrane contactor for separating of gaseous mixture, and mass-transfer efficiency is unstable, assembling difficulty, the shortcomings such as cost is higher.
Summary of the invention
The object of the invention is to for current gas-liquid membrane contactor mass-transfer efficiency unstable, assembling difficulty, the problem that cost is high provides a kind of gas-liquid membrane contactor and applies its mist separation method,
A kind of multichannel gas-liquid membrane contactor, comprise rectangle framework, be fixed on the air cavity plate one between framework upper and lower surface, framework inner chamber is divided into air cavity and sap cavity by described air cavity plate one; The end face homonymy of described air cavity offers gas interface in pairs, the opposite exterior lateral sides face of described sap cavity offers fluidic interface in pairs, also comprise another air cavity plate two, air cavity is divided into two independent sub-air cavitys, described paired gas interface communicates from different sub-air cavitys respectively; Also include hollow-fibre membrane, described hollow-fibre membrane is fixed in film silk stay pipe, and described hollow-fibre membrane two ends is individually fixed on the air cavity plate one of different sub-air cavity along the long limit of framework, and the horizontal segment of described film silk stay pipe is dipped in sap cavity.
Gas-liquid membrane contactor provided by the invention presents shell-and-tube rectangular frame structure, and the hollow-fibre membrane be arranged in film silk stay pipe is tube side, and walk gas, rectangular frame is shell side, walks liquid, and its long limit is effective shell side length.Gas, by hollow-fibre membrane, is entered another sub-air cavity of homonymy, in this process, by liquid, realizes the separation of mist by a sub-air cavity.Whole separation process only realizes in a rectangular frame structure.
As improvement of the present invention, two blocks of air cavity plates one are arranged with in parallel between described framework upper and lower surface, described framework inner chamber is from top to bottom divided into successively, upper gas chamber, sap cavity, lower air chamber, and the air cavity plate two arranged in described upper gas chamber and lower air chamber is divided into two sub-air cavitys respectively.
Thus gas can be passed in the both sides up and down of framework simultaneously, the flow direction of both sides gas can be consistent, also can be inconsistent, thus coordinate with flow direction, realize two following current, two adverse current, or following current adverse current, not only increases separative efficiency, and achieves the separation of multichannel, multi-selection.
As a further improvement on the present invention, the opposite exterior lateral sides face of described sap cavity offers at least two pairs of fluidic interface in pairs, and described fluidic interface forms orthogonal fluid path.That is, on the basis that the flow direction parallel with hollow-fibre membrane is provided, additionally provide the flow direction vertical with hollow-fibre membrane, thus achieve the possibility of cross-flow simultaneously.
Preferred as one, the invention discloses described hollow-fibre membrane is the hollow-fibre membrane adopting polytetrafluoroethylene (PTFE), polypropylene (PP), polyvinylidene fluoride (PVDF) or polyethylene (PE), and described framework is the framework adopting PVC or poly-fluorine class material.
Preferred as one, the invention discloses the length of described rectangle framework: wide: be (8-12): 1.5:1, the wherein high 10cm that is greater than or equal at high proportion, described air cavity height is the 1/10-1/8 of total height.Rectangular length, width and height ratio, particularly Aspect Ratio is larger for the separative efficiency impact of mist, therefore the present inventor is on the basis considering separative efficiency and hollow-fibre membrane self validity, gives (8-12): the preferred proportion of 1.5:1.
Further, described hollow fiber film thread arrangement pitch is 0.5-2cm.To achieve between hollow fiber film thread with liquid effective contacts, and improves mass-transfer efficiency.
As further preferred, described hollow fiber film thread in sap cavity centered by the upper and lower plane of symmetry of framework face symmetrical, the horizontal section length of described hollow fiber film thread is not less than the 45-65% of framework length.Thus ensure that the effective length of hollow fiber film thread, because gas-liquid mass transfer occurs in effective length, so further increase the separating effect of gas-liquid membrane contactor.
Meanwhile, the present invention on the basis of technique scheme, further disclose a kind of its mist be separated in application process, comprise the following steps:
(1) separator is built according to above-mentioned gas-liquid membrane contactor;
(2) select gas interface, form the operator scheme of gas flow process; The operator scheme of described gas flow process is:
(2-1) gas enters a sub-air cavity from a gas interface of gas-liquid membrane contactor side, then through the horizontal segment part of hollow fiber film thread, enter the sub-air cavity of another homonymy, and flow out from another gas interface of homonymy, complete the gas flow process of gas-liquid membrane contactor;
Or
(2-2) gas is with equidirectional or rightabout, entered by a gas interface respectively from the both sides of gas-liquid membrane contactor simultaneously, then through the horizontal segment part of hollow fiber film thread, flow out from another gas interface of this side, complete the gas flow process of gas-liquid membrane contactor;
(3) select fluidic interface, form the operator scheme of liquid flow;
Liquid enters sap cavity from a fluidic interface of gas-liquid membrane contactor side, then flows out from a fluidic interface of gas-liquid membrane contactor opposite side, completes liquid flow;
(4) pass into gas and liquid, complete mist in the mode of following current, adverse current or cross-flow and be separated.
In gas-liquid membrane contactor provided by the present invention, gas-liquid flow process is expressed as: gas enters an air cavity from a gas interface (I) of membrane contactor side, then film silk is entered in stay pipe import, arrive the effective length (sap cavity film silk part) of film silk, gas diffuses in sap cavity solution at this by fenestra, there is mass transfer, the gas not diffusing to sap cavity flows into an air cavity of membrane contactor homonymy along film silk inner chamber, flow out from another gas interface of homonymy (I ') again, complete the gas flow process of membrane contactor side; Or enter by the gas interface (II) of same flow process from this side at membrane contactor opposite side gas simultaneously simultaneously, from another gas interface of this side (II ') outflow, complete the gas flow process of this side equally; The gas flow process of both sides is carried out simultaneously, can be following current (same direction I → I ', II → II ' or I ' → I, II ' → II) operation, also can be adverse current (reverse I → I ', II ' → II or I ' → I, II → II ') operation.Liquid enters sap cavity from a fluidic interface (direction paralleled with gas flow process) of membrane contactor side, absorb and spread the gas of coming from film silk, then flow out from a fluidic interface of membrane contactor opposite side (III '), complete liquid flow, now form advection or counter-current operation with gas.Or liquid enters sap cavity from a fluidic interface (with the direction that gas flow process is perpendicular) of membrane contactor side, absorb and spread the gas of coming from film silk, then flow out from a fluidic interface of membrane contactor opposite side, complete liquid flow, now form cross-flow operation with gas.The operator scheme flowed to has multiple choices, according to the requirement of technique, can arrive energy-efficient object.
The caliber of gas-liquid interface and distribution do not limit, and meet interface fluid flux and equal total fluid flow, and the mouth of pipe is evenly distributed arrival even fluid distribution.
The present invention proposes a kind of multichannel gas-liquid membrane contactor for separating of mist, can be widely used in the fields such as Chemical Engineering, environmental project, food industry and medical industry, is used in particular for separation of C O
2, SO
2, H
2s, NH
3with VOCs and other etc. gas, effectively can avoid the shortcomings such as doughnut distribution density is uneven, shell-side fluid is uneven, be better than existing hollow fiber membrane contactors, separative efficiency improve 20-38%.
By technical scheme disclosed in the present invention, structurally achieve multichannel, more options, packed density is high, apparatus structure is compact, assemble and clear up and optimize easily.Separating effect achieves the optimizations such as mass-transfer efficiency is high, separation costs is low.
Accompanying drawing explanation
Fig. 1 is that the present invention always schemes for separating of the multichannel gas-liquid membrane contactor outward appearance of mist.
Fig. 2 is the multichannel gas-liquid membrane contactor top view of the present invention for separating of mist
Fig. 3 is the multichannel gas-liquid membrane contactor front view of the present invention for separating of mist
Fig. 4 is the multichannel gas-liquid membrane contactor side view of the present invention for separating of mist
Fig. 5 is the multichannel gas-liquid membrane contactor upward view of the present invention for separating of mist
Fig. 6 is the multichannel gas-liquid membrane contactor air cavity partial plan sectional view of the present invention for separating of mist
Fig. 7 is the multichannel gas-liquid membrane contactor sap cavity partial plan sectional view of the present invention for separating of mist
Fig. 8 is the multichannel gas-liquid membrane contactor facade view of the present invention for separating of mist
Wherein:
1-air cavity, 2-sap cavity, 3-film silk stay pipe.
Detailed description of the invention
Below in conjunction with accompanying drawing, the present invention is described in further detail.
It should be noted that, the word "front", "rear" of use is described below, "left", "right", "up" and "down" refer to direction in width figure, word " interior " and " outward " refer to the direction towards or away from particular elements geometric center respectively.
The explanation of embodiment 1 gas-liquid membrane contactor structure
As shown in Figures 1 to 8, a kind of multichannel gas-liquid membrane contactor, comprise rectangle framework as the rectangular structure in Fig. 1, the air cavity plate one be fixed between framework upper and lower surface is illustrated as D1 laminate in the drawings, and framework inner chamber is divided into air cavity 1 and sap cavity 2 by described air cavity plate one D1; The end face homonymy of described air cavity 1 offers gas interface I and I ' in pairs, the opposite exterior lateral sides face of described sap cavity 2 offers fluidic interface III and III ' in pairs, also comprise another air cavity plate two D2, air cavity 1 is divided into two independent sub-air cavitys, described paired gas interface communicates from different sub-air cavitys respectively, that is gas interface I is communicated with the sub-air cavity in left side, and gas interface I ' is connected with the sub-air cavity on right side; Also include hollow-fibre membrane, described hollow-fibre membrane is fixed in film silk stay pipe 3, and described hollow-fibre membrane two ends is individually fixed on the air cavity plate one of different sub-air cavity along the long limit of framework, and the horizontal segment of described film silk stay pipe 3 is dipped in sap cavity 2.Because hollow fiber membrane device is in film silk stay pipe 3, so only represent the position of hollow-fibre membrane in the drawings with film silk stay pipe 3.
In the present embodiment, optimally be arranged with two pieces of air cavity plate one D1 between described framework upper and lower surface in parallel especially, described framework inner chamber is from top to bottom divided into successively, upper gas chamber, sap cavity, lower air chamber, air cavity plate two D2 arranged in described upper gas chamber and lower air chamber is divided into two sub-air cavitys respectively.
Preferably, the opposite exterior lateral sides face of described sap cavity offers at least two pairs of fluidic interface in pairs, and described fluidic interface forms orthogonal fluid path, represents the fluid path perpendicular with gas passage in the drawings with IV and IV '.
Preferably, described hollow-fibre membrane is the hollow-fibre membrane adopting polytetrafluoroethylene (PTFE), polypropylene (PP), polyvinylidene fluoride (PVDF) or polyethylene (PE), and described framework is the framework adopting PVC or poly-fluorine class material.
Embodiment 2
According to different separation case, select different cuboid dimensions, and be equipped with the hollow fiber film thread of applicable material, by it according to preferred separate mode, interval and effective length are set, i.e. horizontal length, and test.
Example 2-1
With reference to shown in Fig. 1-8, a kind of multichannel gas-liquid membrane contactor for separating of mist, its structure: L=100 cm, W=15cm, H=10cm, air cavity D=1.25cm, doughnut PP film silk arrangement pitch is 0.5cm, and the shortest film silk effective length is 50%L.
Operating process: gaseous mixture composition N
2/ CO
2, pressure 0.1MPa, CO
2mole fraction 25%, flow velocity 1.5L/min; Liquid (absorbent) 30%MEA, flow velocity 300mL/min.1) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III → III ', forms adverse current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 28%.2) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III ' → III, forms following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 21%.3) gas-liquid flow process concurrent-countercurrent operation (I → I ', II ' → II); Liquid flow III → III ' or III ' → III, forms inverse following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 25%.4) gas flow process following current operation (I → I ', II → II ') or counter-current operation (I → I ', II ' → II); Liquid flow IV → IV ' or IV ' → IV, forms cross-flow with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 36%.
Example 2-2
With reference to shown in Fig. 1-8, a kind of multichannel gas-liquid membrane contactor for separating of mist, its structure: L=120 cm, W=22.5cm, H=15cm, air cavity D=1.5cm, doughnut PTFE film silk arrangement pitch is 1cm, and the shortest film silk effective length is 65%L.
Operating process: gaseous mixture composition N
2/ CO
2, pressure 0.1MPa, CO
2mole fraction 25%, flow velocity 2L/min; Liquid (absorbent) 30%MEA, flow velocity 400mL/min.1) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III → III ', forms adverse current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 30%.2) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III ' → III, forms following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 22%.3) gas-liquid flow process concurrent-countercurrent operation (I → I ', II ' → II); Liquid flow III → III ' or III ' → III, forms inverse following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 27%.4) gas flow process following current operation (I → I ', II → II ') or counter-current operation (I → I ', II ' → II); Liquid flow IV → IV ' or IV ' → IV, forms cross-flow with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 37%.
Example 2-3
With reference to shown in Fig. 1-8, a kind of multichannel gas-liquid membrane contactor for separating of mist, its structure: L=240 cm, W=30cm, H=20cm, air cavity D=2.2cm, doughnut PP film silk arrangement pitch is 2cm, and the shortest film silk effective length is 45%L.
Operating process: gaseous mixture composition N
2/ CO
2, pressure 0.1MPa, CO
2mole fraction 25%, flow velocity 2.5L/min; Liquid (absorbent) 30%MEA, flow velocity 500mL/min.1) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III → III ', forms adverse current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 30%.2) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III ' → III, forms following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 24%.3) gas-liquid flow process concurrent-countercurrent operation (I → I ', II ' → II); Liquid flow III → III ' or III ' → III, forms inverse following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 28%.4) gas flow process following current operation (I → I ', II → II ') or counter-current operation (I → I ', II ' → II); Liquid flow IV → IV ' or IV ' → IV, forms cross-flow with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 38%.
Example 2-4
With reference to shown in Fig. 1-8, a kind of multichannel gas-liquid membrane contactor for separating of mist, its structure: L=360 cm, W=45cm, H=30cm, air cavity D=3cm, doughnut pvdf membrane silk arrangement pitch is 1.5cm, and the shortest film silk effective length is 50%L.
Operating process: gaseous mixture composition N
2/ SO
2, pressure 0.1MPa, SO
2mole fraction 0.05%, flow velocity 2L/min; Liquid (absorbent) 30% amido citric acid composite solution, flow velocity 600mL/min.1) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III → III ', forms adverse current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 32%.2) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III ' → III, forms following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 25%.3) gas-liquid flow process concurrent-countercurrent operation (I → I ', II ' → II); Liquid flow III → III ' or III ' → III, forms inverse following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 29%.4) gas flow process following current operation (I → I ', II → II ') or counter-current operation (I → I ', II ' → II); Liquid flow IV → IV ' or IV ' → IV, forms cross-flow with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 37%.
Example 2-5
With reference to shown in Fig. 1-8, a kind of multichannel gas-liquid membrane contactor for separating of mist, its structure: L=300 cm, W=37.5cm, H=25cm, air cavity D=2.8cm, doughnut PP film silk arrangement pitch is 0.8cm, and the shortest film silk effective length is 60%L.
Operating process: gaseous mixture composition N
2/ H
2s, pressure 0.1MPa, H
2s mole fraction 0.1%, flow velocity 2L/min; Liquid (absorbent) 30%MDEA, flow velocity 400mL/min.1) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III → III ', forms adverse current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 26%.2) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III ' → III, forms following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 22%.3) gas-liquid flow process concurrent-countercurrent operation (I → I ', II ' → II); Liquid flow III → III ' or III ' → III, forms inverse following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 25%.4) gas flow process following current operation (I → I ', II → II ') or counter-current operation (I → I ', II ' → II); Liquid flow IV → IV ' or IV ' → IV, forms cross-flow with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 36%.
Example 2-6
With reference to shown in Fig. 1-8, a kind of multichannel gas-liquid membrane contactor for separating of mist, its structure: L=450 cm, W=60cm, H=40cm, air cavity D=3cm, doughnut pvdf membrane silk arrangement pitch is 1.2cm, and the shortest film silk effective length is 50%L.
Operating process: gaseous mixture composition N
2/ NH
3, pressure 0.1MPa, NH
3mole fraction 5%, flow velocity 2L/min; Liquid (absorbent) 10%H
2sO
4, flow velocity 400mL/min.1) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III → III ', forms adverse current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 25%.2) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III ' → III, forms following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 20%.3) gas-liquid flow process concurrent-countercurrent operation (I → I ', II ' → II); Liquid flow III → III ' or III ' → III, forms inverse following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 23%.4) gas flow process following current operation (I → I ', II → II ') or counter-current operation (I → I ', II ' → II); Liquid flow IV → IV ' or IV ' → IV, forms cross-flow with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 33%.
Example 2-7
With reference to shown in Fig. 1-8, a kind of multichannel gas-liquid membrane contactor for separating of mist, its structure: L=100 cm, W=15cm, H=10cm, air cavity D=1.25cm, doughnut PTFE film silk arrangement pitch is 0.5cm, and the shortest film silk effective length is 45%L.
Operating process: gaseous mixture composition N
2/ benzene, pressure 0.1MPa, benzene mole divides rate 0.02%, flow velocity 1L/min; Liquid (absorbent) 50% morpholine, flow velocity 200mL/min.1) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III → III ', forms adverse current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 23%.2) gas-liquid flow process following current operation (I → I ', II → II '); Liquid flow III ' → III, forms following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 20%.3) gas-liquid flow process concurrent-countercurrent operation (I → I ', II ' → II); Liquid flow III → III ' or III ' → III, forms inverse following current with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 21%.4) gas flow process following current operation (I → I ', II → II ') or counter-current operation (I → I ', II ' → II); Liquid flow IV → IV ' or IV ' → IV, forms cross-flow with gas, and now compared with the hollow fiber membrane contactors of existing same scale, point rate efficiency improves 28%.
technology assessment result is as follows:
Result shows, a kind of multichannel gas-liquid membrane contactor for separating of mist that the present invention proposes can improve a point rate efficiency effectively, is a kind of high performance membrane assembly.
Claims (7)
1. a multichannel gas-liquid membrane contactor, is characterized in that described gas-liquid membrane contactor comprises rectangle framework, is fixed on the air cavity plate one between framework upper and lower surface, and framework inner chamber is divided into air cavity and sap cavity by described air cavity plate one; The end face homonymy of described air cavity offers gas interface in pairs, the opposite exterior lateral sides face of described sap cavity offers fluidic interface in pairs, also comprise another air cavity plate two, air cavity is divided into two independent sub-air cavitys, described paired gas interface communicates from different sub-air cavitys respectively; Also include hollow-fibre membrane, described hollow-fibre membrane is fixed in film silk stay pipe, and described hollow-fibre membrane two ends is individually fixed on the air cavity plate one of different sub-air cavity along the long limit of framework, and the horizontal segment of described film silk stay pipe is dipped in sap cavity;
The opposite exterior lateral sides face of described sap cavity offers at least two pairs of fluidic interface in pairs, and described fluidic interface forms orthogonal fluid path.
2. gas-liquid membrane contactor according to claim 1, it is characterized in that: between described framework upper and lower surface, be arranged with two blocks of air cavity plates one in parallel, described framework inner chamber is from top to bottom divided into successively, upper gas chamber, sap cavity, lower air chamber, the air cavity plate two arranged in described upper gas chamber and lower air chamber is divided into two sub-air cavitys respectively.
3. gas-liquid membrane contactor according to claim 1, it is characterized in that: described hollow-fibre membrane is the hollow-fibre membrane adopting polytetrafluoroethylene (PTFE), polypropylene (PP), polyvinylidene fluoride (PVDF) or polyethylene (PE), described framework is the framework adopting PVC or poly-fluorine class material.
4. gas-liquid membrane contactor as claimed in any of claims 1 to 3, it is characterized in that: the length of described rectangle framework: wide: be (8-12): 1.5:1 at high proportion, wherein highly be greater than or equal to 10cm, described air cavity height is the 1/10-1/8 of total height.
5. gas-liquid membrane contactor as claimed in any of claims 1 to 3, is characterized in that: hollow fiber film thread arrangement pitch is 0.5-2cm.
6. gas-liquid membrane contactor according to claim 2, is characterized in that: hollow fiber film thread in sap cavity centered by the upper and lower plane of symmetry of framework face symmetrical, the horizontal section length of described hollow fiber film thread is not less than the 45-65% of framework length.
7. a mist separation method, is characterized in that comprising the following steps:
(1) separator is built according to the gas-liquid membrane contactor in claim 1 to 6 described in any one;
(2) select gas interface, form the operator scheme of gas flow process; The operator scheme of described gas flow process is:
(2-1) gas enters a sub-air cavity from a gas interface of gas-liquid membrane contactor side, then through the horizontal segment part of hollow fiber film thread, enter the sub-air cavity of another homonymy, and flow out from another gas interface of homonymy, complete the gas flow process of gas-liquid membrane contactor;
Or
(2-2) gas is with equidirectional or rightabout, entered by a gas interface respectively from the both sides of gas-liquid membrane contactor simultaneously, then through the horizontal segment part of hollow fiber film thread, flow out from another gas interface of this side, complete the gas flow process of gas-liquid membrane contactor;
(3) select fluidic interface, form the operator scheme of liquid flow;
Liquid enters sap cavity from a fluidic interface of gas-liquid membrane contactor side, then flows out from a fluidic interface of gas-liquid membrane contactor opposite side, completes liquid flow;
(4) pass into gas and liquid, complete mist in the mode of following current, adverse current or cross-flow and be separated.
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| CN103342623A (en) * | 2013-05-07 | 2013-10-09 | 石河子大学 | Method and system of separating and purifying acetylene in gas mixture from plasma pyrolysis coal by using hollow fiber membrane contactor |
| EP3501627A4 (en) * | 2016-08-18 | 2020-04-01 | Toyobo Co., Ltd. | Flat hollow fiber membrane module and membrane separation unit |
| CN115546197A (en) * | 2022-11-08 | 2022-12-30 | 东莞理工学院 | Quantitative analysis method for distribution characteristics of randomly distributed hollow fiber membrane modules |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5230796A (en) * | 1990-01-03 | 1993-07-27 | Nederlandse Organisatie Voor Toegepastnatuurwetenschappelijk Onderzoek Tno | Transfer device for the transfer of matter and/or heat from one medium flow to another medium flow |
| CN101362044A (en) * | 2008-09-08 | 2009-02-11 | 江南大学 | Formaldehyde exhaust-gas efficient film absorption technique |
| CN101584960A (en) * | 2008-05-22 | 2009-11-25 | 青岛生物能源与过程研究所 | Separator and separation and purification method of gas-liquid phase absorbing membrane |
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| JP2000185212A (en) * | 1998-12-22 | 2000-07-04 | Ube Ind Ltd | Method for separating and recovering perfluoro compound gas and device therefor |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5230796A (en) * | 1990-01-03 | 1993-07-27 | Nederlandse Organisatie Voor Toegepastnatuurwetenschappelijk Onderzoek Tno | Transfer device for the transfer of matter and/or heat from one medium flow to another medium flow |
| CN101584960A (en) * | 2008-05-22 | 2009-11-25 | 青岛生物能源与过程研究所 | Separator and separation and purification method of gas-liquid phase absorbing membrane |
| CN101362044A (en) * | 2008-09-08 | 2009-02-11 | 江南大学 | Formaldehyde exhaust-gas efficient film absorption technique |
Non-Patent Citations (1)
| Title |
|---|
| Hollow fiber modules made with hollow fiber fabric;S.R. Wickramasinghe 等;《Journal of Membrane Science》;19931231;第84卷(第1-2期);摘要、第3页第1栏第3行-第5页第1栏第36行及图1 * |
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